MXPA98007589A - Bimetallic catalyst for the simultaneous selective hydrogenation of diolephins and nitrile, and method to manufacture my - Google Patents

Abstract

A useful catalyst is provided for the simultaneous or selective hydrogenation of diolefins and nitriles present in a hydrocarbon feedstock including: (a) a support material which is selected from the group consisting of inorganic oxide, carbon, zeolite and mixtures thereof; and (b) a catalytically active metal phase which includes at least two metals which are selected from the group consisting of at least partially reduced group IB metals and completely reduced group VII metals, the active metal phase is present in a amount of about > _0.03% in pe

Description

- i - BIMETALLIC CATALYST FOR THE SIMULTANEOUS SELECTIVE HYDROGENATION OF DIOLEPHINS AND NITRILE, AND METHOD TO MANUFACTURE THE SAME BACKGROUND OF THE INVENTION The present invention relates to a bimetallic catalyst material for use in the hydrogenation of hydrocarbon feedstocks and, more particularly, to a catalyst which is useful for the simultaneous and selective hydrogenation of diolefins and nitriles present in a hydrocarbon feedstock . In the prior art processes and catalysts for hydrogenating unsaturated compounds in liquid hydrocarbon feedstocks are known. For example, U.S. Patent No. 4,152,351 describes a process for the hydrogenation of an olefinic unsaturation. More specifically, it relates to the catalytic hydrogenation of an unsaturated aliphatic compound in the presence of a palladium hydrogenation catalyst in a suitable support. Even more specifically, the invention relates to the use of applicable additives for a palladium hydrogenation catalyst used to hydrogenate the olefinic unsaturation. In addition, the invention relates to the hydrogenation of aliphatic unsaturated compounds containing nitrile groups. U.S. Patent No. 4,271,323 discloses a process for hydrogenating unsaturated compounds in liquid phase, in the presence of a soluble catalyst obtained by reacting an organometal derivative or a metal hydride with a synergistic mixture of: (a) a zinc compound, zirconium, manganese, molybdenum or iron, and (b) a nickel or cobalt compound. U.S. Patent No. 4,734,540 describes a process which is useful for the selective hydrogenation of polyunsaturated organic compounds. The product resulting from such reaction produces the monoolefin equivalents of the hydrogenated polyunsaturated organic compounds. The catalyst used in this selective hydrogenation process comprises nickel and sulfur deposited on the surface of an alumina support. The preferred catalyst does not contain halogens, noble metals, alkaline earth metals or alkali metals and is characterized in that it only has a very low percentage of total pore volume provided by pores having an average pore diameter of less than 150 angstroms. The vast majority of the pore volume is present in the form of macropores having diameters of 500 to 1500 angstroms. Although the preceding process uses catalysts which are useful in the hydrogenation process, the process and the catalyst are neither selective nor hydrogenated simultaneously of olefins and nitriles. Naturally, it would be highly desirable to provide a catalyst which is useful for the simultaneous selective hydrogenation of diolefins and nitriles in a hydrocarbon feedstock. Accordingly, it is the main object of the present invention to provide a catalyst useful for the simultaneous and selective hydrogenation of diolefins and nitriles present in a hydrocarbon feedstock. A further objective of the present invention is to provide a method for preparing a catalyst as mentioned in the foregoing. A further objective of the present invention is to provide a process for the simultaneous and selective hydrogenation of diolefins and nitriles from a hydrocarbon feedstock using such a catalyst. Another object of the present invention is to provide a bimetallic catalyst for the simultaneous selective hydrogenation of diolefins and nitriles, a method for manufacturing such bimetallic catalyst and a process using such a catalyst. Further objects and advantages of the present invention will appear in the following.

BRIEF DESCRIPTION OF THE INVENTION The present invention relates to a catalyst useful for the simultaneous and selective hydrogenation of diolefins and nitriles present in a hydrocarbon feedstock.

Preferably, the support material is selected from the group consisting of an inorganic oxide-zeolite composite material, carbon and zeolite. A catalytically active phase is deposited on the support material. The catalytically active metallic phase is selected from the group consisting of partially reduced group IB metals and completely reduced group VIII metals. The catalytically active metallic phase is present in an amount of = 0.03% by weight. According to a preferred embodiment of the present invention, the catalytically active phase preferably comprises at least two active metals which are selected from the group comprising partially reduced group IB metals and completely reduced group VIII metals. The catalyst of the present invention is particularly useful in a process for the simultaneous and selective hydrogenation of diolefins and nitriles present in a hydrocarbon feedstock. The catalyst of the present invention is prepared by impregnating the support material with a solution of the active metal phase, drying the impregnated support and calcining. The calcined dried support is subsequently activated at the appropriate reduction state. The catalyst is used in a hydrogenation process where the hydrocarbon feedstock in the presence of the catalyst and hydrogen is treated at a temperature between about 50 and 250 ° C and a pressure of 10.5 to 46 kg / cm2 (150 to 650 psi) ) so that it selectively hydrogenates olefins and nitriles from the hydrocarbon feedstock. The bimetallic catalyst of the present invention is preferably prepared by impregnating the support material with a single solution containing all the desired group VIII metals, and / or by incorporation of group IB metals by successive impregnation with intermediate calcination and activation after each stage of impregnation.

DETAILED DESCRIPTION The catalyst of the present invention is particularly useful in a process for the simultaneous selective hydrogenation of diolefins and nitriles. The catalyst of the present invention comprises a support material having a catalytically active metallic phase deposited thereon. Suitable support materials include inorganic oxide-zeolite, carbon and zeolite compounds. Preferably, the support material is selected from the group consisting of inorganic oxides, carbon, zeolite and mixtures thereof. Suitable inorganic oxides are selected from the group consisting of silica, alumina, clay, titania, magnesia and mixtures thereof, as well as other molecular sieve materials and the like. Particularly suitable support materials include zeolite-clay and alumina-zeolite.

The support material has deposited thereon a catalytically active metallic phase which is selected from the group consisting of metals of group IB and metals of group VIII of the Periodic Table. Based on the active metal used, the amount of metallic active phase present on the catalyst can vary. The active metal should be present in a minimum amount of about = 0.03% by weight up to 25% by weight. Particularly active and suitable metallic materials include copper, nickel, iron, cobalt and palladium. Preferably, the metal active phase includes at least two metals which are selected from the group consisting of completely reduced group VIII metals and partially reduced group IB metals. Particularly suitable combinations of active metals include nickel / copper, nickel / cobalt and nickel / iron. According to the present invention, it has been found that the bimetallic catalyst according to the present invention, having two different metals selected from group VIII and group IB metals, provide excellent operation in processes for selective and simultaneous hydrogenation of diolefins and nitriles. As indicated before, a support material particularly suitable for use in the catalyst of the present invention is an alumina-zeolite compound. It has been found that the surface area of the resulting catalyst should be between about 100 and 1500 m2 / g, preferably between 100 to 1000 m2 / g and ideally between about 250 to 350 m2 / g. The pore volume of the catalyst is preferably between 0.20 cc / g to 1.50 cc / g, preferably between 0.30 cc / g and 0.70 cc / g. In order that the catalyst of the present invention be effective in the simultaneous selective hydrogenation of diolefins and nitriles, it has been found that the metal active phase must be reduced to the correct state in order to be effective. According to the present invention, the metals of group IB must be partially reduced, while the metals of group VIII must be completely reduced. By partial reduction it is meant that the metal sites consist of one or more non-zero oxidation states, more particularly metal sites that show catalyst with a net charge on them. By complete reduction it is meant that the metal sites consist mainly of single species, more particularly the higher number of samples present the elementary state of the charge, that is, zero. In accordance with the preferred embodiment of the present invention wherein at least two metals are provided, the calcination and activation are controlled with caution so as to provide partially reduced Group IB metals and completely reduced Group VIII metals, as desired.

The catalyst of the present invention is prepared by impregnating the support material with a solution containing the catalytically active metal phase, for example, in the form of metal salts. As indicated in the above, the active metal phase must be present in an amount above the final catalyst of about = 0.03% by weight. Subsequently, the impregnated support material is dried and calcined at a temperature between 150 and 600 ° C for a sufficient time to decompose the impregnated metal salt on the catalyst support. Particularly suitable metal salts used in the aqueous solution to impregnate the catalyst material include Cu (N03) 2 * 2.5 H20; (NiN03) 2 * 6H20; Y (CH3C00) 2Pd, although other solutions can be used. The dry and calcined catalyst is subsequently activated at the appropriate reduction state based on the type of active metal phase used. The partial reduction of group IB metals is carried out under the following conditions: temperature (° C) 150-300, pressure (kg / cm2 (psi)) 1.05-25 (15-350), flow rate of H2 (1 / h) 0.1-8.0. The complete reduction of group VIII is carried out under the following conditions: temperature (° C) 200-600, pressure (kg / cm2 (psi)) 1.05-25 (15-350), flow rate of H2 (1 / h) 0.1-8.0. Generally, it is preferred that the temperature be less than about 350 ° C and that the pressure be less than about 18 kg / cm2 (250 psi) for partial reduction, and that the temperature be greater than about 400 ° C and the pressure be higher of approximately 18 kg / cm2 (250 psi) for total reduction. In relation to the preparation of the bimetallic catalyst according to the present invention, when two or more group VIII metals are to be impregnated on the support, it is preferred that these metals are deposited on the support material by impregnation with a unique solution which contains each of the desired group VIII metals. If the active metal phase of the bimetallic catalyst according to the present invention is to contain one or more metals of group IB, it is preferred that the group IB metal is incorporated or impregnated onto the support material separately, preferably after the Group VIII metals, by successive impregnation using a solution of the group IB metal. If more than one group IB metal is to be used, each metal must be impregnated using a separate solution. Preferably, each successive impregnation is followed by intermediate calcination and activation to the desired reduction state. In general, it is preferred that the support be impregnated first with a solution containing any metal or metals of group VIII to be used, followed by calcination and activation to at least partially reduce the metal or metals of group VIII, and then Any Group IB metal is impregnated on the catalyst impregnated with the Group VIII metal, followed again by calcination and activation in a manner which reduces part of the Group IB metal, as desired, and the complete reduction of the metal or metals of the group. group VIII. However, it has been found that when zeolite-alumina is used as a support, the support can first be impregnated with the group IB metal, calcined and activated at partial reduction of the group IB metal, followed by impregnation with metal or metals. of group VIII, and calcination and activation to completely reduce the metal or metals of group VIII. In this case, it has been found that the support alumina stabilizes the partially reduced group IB metal species so that the group IB metal remains partially reduced through the complete reduction of the group VIII metal or metals. Other impregnation sequences can be used which include, for example, co-impregnation, but the successive impregnations described above are preferred. For the preferred bimetallic catalyst of the present invention, metals are preferably provided having a metallic atomic ratio in the range of from 1: 100 to about 100: 1, based on the metals to be used, and the total metallic content is preferably between about 0.03% by weight up to about 25% by weight based on the total weight of the final catalyst. Furthermore, as stated above, the metals of the bimetallic catalyst according to the present invention can be partially reduced adequately by treating the catalyst at a temperature of less than or equal to about 350 ° C, at a pressure of less than or equal to 18 kg / cm2 (250 psi) and for a time of less than about 15 hours, while the catalyst can suitably be reduced completely or completely through a treatment at temperatures above 400 ° C and pressures of hydrogen of more than about 18 kg / cm2 (250 psi) and for periods of time of at least about 8 hours. The catalyst of the present invention prepared according to the method described above is particularly useful in processes for the simultaneous and selective hydrogenation of diolefins and nitriles from a hydrocarbon feedstock. The hydrocarbon feedstock in the presence of catalyst is mixed with hydrogen wherein the ratio of hydrogen to diolefins and nitriles in the feedstock is less than three times the stoichiometric amount needed to selectively hydrogenate diolefins and nitriles. The hydrogen, the hydrocarbon feedstock and the catalyst are treated in a reactor at a temperature of between 50 to 250 ° C at a pressure of between 10.5 to 46 kg / cm2 (150 to 650 psi). The preferred conditions for the hydrogenation process are a temperature of between 70 to 160 ° C and a pressure of between 14 to 28 kg / cm2 (200 to 400 psi) at a space velocity per hour of liquid of between 0.1 to 5 h "1, preferably 0.5 to 5 h" 1, ideally 1 to 4.5 h "1. The advantageous characteristics of the catalyst of the present invention and method for preparing it will become apparent from the following examples.

EXAMPLE 1 This example demonstrates the process for making the catalyst of the present invention using an inorganic oxide-zeolite compound as a support having an activated metal phase of group VIII deposited thereon. The alumina-zeolite composite material backing of the type described in U.S. Patent No. 4,762,537 and sold by Alcoa Aluminum Corporation under the trademark Selexsorb is selected as the catalyst support material. Four of the catalyst supports are impregnated with nickel nitrate solutions of different concentrations. A fifth catalyst is prepared by impregnating the catalyst support with palladium. The five impregnated catalysts are dried and calcined so as to decompose the salts of the incorporated active metal. The impregnated and calcined catalyst supports are then activated under controlled temperature and time conditions so that they completely reduce or partially reduce the active metal phase. For complete reduction, the catalyst is treated at a temperature of 450 ° (at 18 kg / cm2 (250 psi) for 8 hours.) The partial reduction is carried out at 250 ° C for 8 hours at 14 kg / cm2 (200 psi). Table 1 below is established for a catalyst composition and an activation treatment for each of the five catalysts.

Table 1 Catalyst Support Active target phase Alumina activation- 0.93% by weight of Ni completely reduced zeolite alumina- 5.7% by weight of Ni completely zeolite reduced by alumina- 5.7% by weight of Ni partially reduced zeolite alumina- 12.90% by weight of Ni completely zeolite reduced alumina- 0.30% by weight of Pd completely reduced zeolite EXAMPLE 2 This example demonstrates the catalytic activity for the catalysts of Example 1 for the simultaneous and selective hydrogenation of diolefins and nitriles present in hydrocarbon feedstocks. The activity for simultaneous selective hydrogenation was determined during a 4 hour test using a synthetic C5 hydrocarbon feedstock having the composition set forth in Table 2.

Table 2 Composition of synthetic raw material C5 97.5% Propionitrile 0.5% Diolefins 0.5% Monoolefins 1.0% Eight cc of each of the activated catalysts set forth in Example 1 were used in a reactor to treat the hydrocarbon feedstock of Table 2. The reaction took place for 3 hours at a temperature of 120 ° C and a pressure of 18 kg / cm2 (250 psi). The volume ratio of hydrogen fed to the reactor with respect to the diolefins and nitriles was maintained at 3. The liquid space velocity (LHSV) of the hydrogen feed is adjusted to 3 h "1. The results for each test using the catalysts of Example 1 are set forth herein below, in Table 3.

Table 3 Catalyst% conversion% conversion% conversion of diolefins monoolefins nitrile sion 1 100 59 86 2 100 78 100 3 0 0 0 4 100 0 100 100 0 88 As can be seen from Table 3, the concentration of the active metal phase of group metals VIII used has an effect on the selective hydrogenation of diolefins and nitriles in the hydrocarbon. Nickel concentrations of less than 6% by weight are insufficient to ensure selective hydrogenation. The catalyst 1 having a nickel concentration of 0.93% by weight was in fact not selective. At the same time, as can be seen from the results using catalyst 5, 0.3% by weight of palladium is sufficient to ensure selective hydrogenation of diolefins and nitriles. Furthermore, when comparing the results obtained from the hydrogenation of raw materials with catalysts 4 and 3, it can be seen that the metals of group VIII must be completely reduced in order that the catalyst is active for the hydrogenation of diolefins and nitriles. Specifically, catalyst 3, which contained 5.7% by weight of nickel, partially reduced, does not obtain any conversion of olefins, monoolefins or nitriles.

EXAMPLE 3 This example demonstrates the process for making the catalyst of the present invention using an inorganic oxide-zeolite composite support having an active metal phase of group IB deposited thereon. Three supports of alumina-zeolite composite material were impregnated with copper nitrate solutions of different concentrations. The three impregnated catalysts were dried and calcined so that the salt of the active metal incorporated was decomposed. Two of the impregnated and calcined catalyst supports were activated by carrying out the partial reduction of the active metal phase at 250 ° C for three hours. The third impregnated catalyst support was completely reduced under the same conditions set forth in Example 1. Table 4 below establishes the catalyst composition and the activation treatment for each of the three catalysts.

Table 4 Catalyst Support Active metal phase Activation 6 alumina- 0.79% by weight of Cu partially reduced zeolite alumina- 5.9% by weight of Cu completely zeolite reduced alumina- 5.8% by weight of Cu completely reduced zeolite EXAMPLE 4 This example demonstrates the catalyst activity for the catalysts of Example 3 for simultaneous and selective hydrogenation of diolefins and nitriles present in the hydrocarbon feedstocks. The synthetic raw material set forth in Table 2 of Example 2 is processed using the catalysts of Example 3 under the same conditions described above as in Example 2. The result of each test using the catalysts of Example 3 is set forth in the following , in Table 5.

Table 5 Catalyst% conversion% conversion% conversion of diolefins monoolefins nitrile 6 98 0 21 7 99 0 82 8 0 0 0 As can be seen from Table 5, as is the case with the Group VIII metals described above, the concentrations of the active metal phase of the Group IB metals used have an effect on the selective hydrogenation of diolefins and nitriles in the hydrocarbon. Copper concentrations as low as 0.80% by weight were effective for selective and simultaneous hydrogenation of diolefins and nitriles. In addition to the above, the degree of reduction of the metallic phase affects the activity of the group IB metal. However, contrary to group VIII metals, Group IB metals are effective when they are partially reduced and ineffective when they are completely reduced. In this regard, see catalyst No. 8, in which the metallic copper phase is completely reduced and there is no conversion of diolefins, monoolefins or nitriles.

EXAMPLE 5 This example shows the importance of the catalyst support on the activity of the catalyst of the present invention. Carbon granules provided by Johnson Matthey are selected as a catalyst support. A second catalyst support comprises gamma alumina sold by Johnson Matthey which was also selected in the same way. Both supports were impregnated with palladium in the manner described above with respect to Example 1 and the impregnated catalyst supports then activated complete reduction at a temperature of 450 ° C, a pressure of 18 kg / cm2 (250 psi) for eight hours. Table 6 below establishes the catalyst composition and the activation treatment for each of the two catalysts.

Table 6 Catalyst Support Active metal phase Activation 9 alumina- 1.0% by weight of Pd completely reduced zeolite carbon 0.3% by weight of completely reduced Pd 11 gamma- 0.3% by weight of Pd completely reduced alumina EXAMPLE 6 In order to demonstrate the activity of the catalyst for the catalysts of Example 5 for the simultaneous and selective hydrogenation of diolefins and nitriles, the synthetic raw material of Example 2 was treated with the catalyst under the same conditions set forth in Example 2. Results for each test using the catalysts of Example 5 are set forth below in Table 7.

Table 7 Cataliz;% conversion rate% conversion% conversion of diolefins of monoolefins nitrile 9 100 88 18 100 0 50 11 100 30 20 The carbon-supported catalyst, catalyst 10, is effective for the simultaneous hydrogenation of diolefins and nitriles in a selective manner wherein the supported catalysts in the alumina (9 and 11) do not achieve selective compression of diolefins, monoolefins or nitriles. The result leads to the conclusion that the carbon and the zeolite present in the inorganic oxide-zeolite composition are effective as catalyst supports for the catalysts of the present invention. Both the zeolite and the carbon contain moderate Lewis acid sites which are believed to be responsible for the higher activity characteristics of the catalysts of the present invention.

Example 7 This example illustrates the bimetallic catalyst preparation method according to the present invention, using a mixture of zeolite and alumina or zeolite and clay as support for the metal phases that include only nickel / copper, nickel / cobalt and nickel / iron. The support is previously calcined. The metal or group VIII metals are deposited by impregnation from a solution. The group IB metal is subsequently impregnated successively on the support using a solution of the group IB metal, with calcination or intermediate activation after each impregnation under conditions to partially reduce the group IB metal and completely reduce the metal or metals of group VIII . Each catalyst contains 8% by weight of total metal. The impregnated catalysts are activated by carefully controlling the time and temperature in order to obtain total or partial reduction, as desired. For a total reduction, the catalyst is treated at a temperature above 400 ° C, hydrogen pressures greater than 18 kg / cm2 (250 psi) and for a longer time of 8 hours. For partial reduction, the catalysts are treated at temperatures lower than 350 ° C, pressure lower than 18 kg / cm2 (250 psi) and for a shorter time of 15 hours. The catalysts prepared as set forth above are further described in Table 8 below. This example also illustrates the catalytic performance of the catalysts prepared as above, using a C5 naphtha feedstock containing 2% by weight of dienes and 50 ppmv of nitriles. 25 cc samples of each catalyst were used in a fixed bed reactor. The raw material is hydrogenated at 120 ° C, 18 kg / cm2 (250 psi) and LHSV = 1 h "1. The conversion is evaluated after 6 hours in the stream and the results are set forth in Table 8 below.

Table 8 Catalyst Proportion Support Dienes Nitrile metal (%) (%) Ni - zeolite - 75 73 clay Ni / Cu 1: 1 zeolite - 96 79 clay Ni / Cu 1: 2 zeolite - 83 77 clay Ni / Cu 2: 1 zeolite - 92 74 clay Ni / Cu 2: 1 zeolite- 100 95 alumina Ni / Cu 7: 1 zeolite- 95 97 alumina Ni / Cu 40: 1 zeolite- 91 89 alumina Ni / Co. 1: 1 zeolite- 88 93 clay Ni / Fe 1: 1 zeolite- 80 94 clay Ni / Fe 1: 2 zeolite- 80 42 clay Ni / Fe 2: 1 zeolite- 89 82 clay As shown, the operation of a bimetallic catalyst of the present invention is superior to that of a monometallic catalyst.

Example 8 The example shows the activity of completely reduced catalyst to treat the same raw material under the same conditions as in Example 7. Catalysts were prepared using nickel, nickel / copper, nickel / cobalt and nickel iron, and each catalyst including nickel / copper It was completely reduced. The results are set forth in Table 9 below.

Table 9 Catalyst Proportion Dienes Metal nitrile (%) (%) Ni - zeolite - 100 97 clay Ni / Cu 2: 1 zeolite - 77 79 clay Ni / Co 2: 1 zeolite - 100 100 clay Ni / Fe 2: 1 zeolite - 100 100 clay As shown, excellent results are obtained using completely reduced Group VIII metals. However, operation suffers when the bimetallic catalyst of the HIV / group IB group, including the group IB metal, is completely reduced.

Example 9 This example illustrates the use of catalysts prepared as set forth in Example 7 according to the invention to treat a raw material having nitrile content increased four times, treated under the same conditions as in Example 7. The results are set forth in Table 10 below.

Table 10 Catalyst Proportion Support Dienes Nitrile metal (%) (%) Ni - zeolite - 100 73 clay Ni / Cu 2: 1 zeolite - 100 100 alumina Ni / Co 2: 1 zeolite - 100 100 clay As shown, even at increased levels of nitriles, excellent results are obtained using the bimetallic catalyst in accordance with the invention Example 10 This example shows the effect of the impregnation sequence on the operation of the catalyst for treating the raw material of Example 7, using partially reduced catalysts. The catalysts were prepared using nickel and coimpregnated copper, nickel and copper successively impregnated, and copper and then nickel impregnated successively. The catalysts were calcined and then reduced after each impregnation step to the appropriate conditions for each type of metal. After the final activation, the catalysts were used to treat the raw material set forth in the above under the conditions of Example 7. The results are set forth below, in Table 11.

Table 11 Catalyst Proportion Support Dienes Nitrile metal (%) (%) Ni / Cu 2: 1 zeolite- 100 97 (coimp) clay Ni / Cu 2: 1 zeolite- 100 100 clay Cu / Ni 2: 1 zeolite- 77 79 clay As shown above, the order of impregnation as well as the presence of the second metal during calcination can modify the reproducibility of the metals. As shown, impregnation with the group VIII metal first provides a partially reduced group IB and completely reduced group VIII metals, as desired, and better results are obtained with this catalyst (Ni / Cu). This invention may be embodied in other forms or may be carried out in other ways without departing from spirit or the essential characteristics of it. Therefore, the present embodiment is considered in all aspects illustrative and not limiting, the scope of the invention is indicated by the appended claims, and all changes which are within the meaning and scope of equivalence are intended to be encompassed for the same.

Claims (26)

1. A catalyst useful for the simultaneous and selective hydrogenation of diolefins and nitriles present in a hydrocarbon feedstock, the catalyst is characterized in that it comprises: (a) a support material that is selected from the group consisting of inorganic oxide, carbon, zeolite and mixtures thereof, - and (b) the catalytically active metallic phase comprising at least two metals which are selected from the group consisting of partially reduced group IB metals and fully reduced group VIII metals, the active metal phase is present in an amount of about = 0.03% by weight.

2. The catalyst according to claim 1, characterized in that the support material is an inorganic oxide which is selected from the group consisting of silica, alumina, clay, titania, magnesia and mixtures thereof.

3. The catalyst according to claim 1, characterized in that the support material is an alumina-zeolite composite material.

4. The catalyst according to claim 3, characterized in that the surface area of the catalyst is between approximately 100 and 1500 m2 / g.

5. The catalyst according to claim 3, characterized in that the surface area of the catalyst is between approximately 100 and 1000 m2 / g.

6. The catalyst according to claim 3, characterized in that the surface area of the catalyst is between approximately 250 and 350 m2 / g.

7. The catalyst according to claim 3, characterized in that the pore volume of the catalyst is between about 0.20 cc / g and 1.50 cc / g.

8. The catalyst according to claim 3, characterized in that the pore volume of the catalyst is between approximately 0.30 cc / g and 0.70 cc / g.

9. The catalyst according to claim 1, characterized in that the active metal phase is present in an amount between approximately 0.03 and 25% by weight.

10. The catalyst according to claim 1, characterized in that the metal of group VIII is selected from the group consisting of nickel, iron, cobalt, palladium and mixtures thereof, and the metal of group IB is copper.

11. The catalyst according to claim 1, characterized in that the active metal phase is nickel and copper.

12. The catalyst according to claim 1, characterized in that the active metal phase is nickel and cobalt.

13. The catalyst according to claim 1, characterized in that the active metal phase is nickel and iron.

14. A method for preparing a catalyst useful for the simultaneous and selective hydrogenation of diolefins and nitriles present in a hydrocarbon feedstock, the method is characterized in that it comprises the steps of: (a) providing a support material that is selected from the group consisting of of inorganic oxide, carbon, zeolite and mixtures thereof, - (b) impregnating the support material with a salt of a catalytically active metal phase comprising at least two metals which are selected from the group consisting of group IB metals and Group VIII metals, the active metal phase is present in an amount of about = 0.03% by weight based on the final catalyst; and (c) calcining and activating the impregnated support at a temperature between about 150 ° C and about 650 ° C so as to completely reduce the metals of group VIII and partially reduce the metals of group IB.

15. The method according to claim 14, characterized in that the impregnation step comprises impregnating the support material with metal salts of at least two metals, and drying for a sufficient time to decompose the metal salts impregnated in the support.

16. The method according to claim 14, characterized in that the step of impregnation of metal comprises impregnating the support material with the metal of group VIII so as to provide a support impregnated with metal of group VIIIcalcining the impregnated support of metal VIII so as to at least partially reduce the metal of group VIII, impregnate the support impregnated with group VIII, with a metal of group IB so as to provide a final impregnated support, and calcinate the support final impregnated, so the metal of group VIII is completely reduced and the metal of group IB is partially reduced.

17. The method according to claim 14, characterized in that the activation step of the metal comprises activating at a temperature of (° C) 200-600, a pressure (kg / cm2 (psi)) of 1.05-25 (15-350) and a flow rate H2 (1 / h) of 0.1-8.0 in a manner that completely reduces the metals of group VIII.

18. The method according to claim 14, characterized in that the activation step comprises activating at a temperature of (° C) 150-300, a pressure (kg / cm2 (psi)) of 1.05-25 (15-350) and a flow rate of H2 (1 / h) of 0.1-8.0 so that it partially reduces to the metals of group IB.

19. The method according to claim 17, characterized in that the activation step comprises activating at a temperature of (° C) 150-300, a pressure (kg / cm2 (psi)) of 1.0-25 (15-350), and a flow rate of H2 (1 / h) of 0.1-8.0 so that it partially reduces the metal of group IB.

20. The method according to claim 14, characterized in that the support material is zeolite-alumina, and wherein the impregnation step comprises impregnating the support material with the group IB metal so as to provide a support impregnated with metal of the group IB, calcining the support impregnated with group IB metal so as to partially reduce the metal of group IB, impregnate the support impregnated with group IB metal with group VIII metal so as to provide a final impregnated support, and calcinate the support final impregnated- so as to completely reduce the metal of group VIII so that the metal of group IB remains partially reduced.

21. A process for the simultaneous and selective hydrogenation of diolefins and nitriles from a hydrocarbon feedstock, the process is characterized in that it comprises the steps of: (a) providing a hydrocarbon feedstock having a diolefin content of > 0.1% by weight and a nitrile content of = 2 ppm (v), - (b) provide a catalyst comprising: 1) a support material that is selected from the group consisting of inorganic oxide, carbon, zeolite and mixtures of the same, - and 2) a catalytically active metallic phase comprising at least two metals that are selected from the group consisting of partially reduced group IB metals and completely reduced group VIII metals, the active metal phase is present in a amount of approximately = 0.03% by weight, (c) mixing the hydrocarbon feedstock in the presence of the catalyst with hydrogen wherein the ratio of hydrogen to diolefins and nitriles in the raw material is less than three times the stoichiometric amount required for selectively hydrogenate diolefins and nitriles; and (d) treating the raw material and the hydrogen mixture in the presence of the catalyst at a temperature of about 50 to 250 ° C at a pressure of between approximately 10.5 to 46 kg / cm2 (150-650 psi).

22. The process according to claim 1, characterized in that the temperature is between about 60 and 160 ° C.

23. The process according to claim 21, characterized in that the pressure is between 14 and 28 kg / cm2 (200-400 psi).

24. The process according to claim 21, characterized in that the space velocity per hour of liquid is in the range of between about 0.1 and 5 h_1.

25. The process according to claim 21, characterized in that the space velocity per hour of liquid is in the range of between about 0.5 and 5 h "1.

26. The process according to claim 21, characterized in that the space velocity per hour of liquid is in the range of between about 1 and 4.5? TX.